Addition of a Base to Enhance Product Yield in Alkylation Reactions

ABSTRACT

A process for making styrene including providing toluene, a co-feed, and a C 1  source to a reactor containing a catalyst having acid sites and reacting toluene with the C 1  source in the presence of the catalyst and the co-feed to form a product stream containing ethylbenzene and styrene, wherein the C 1  source is selected from methanol, formaldehyde, formalin, trioxane, methylformcel, paraformaldehyde, methylal, dimethyl ether, and wherein the co-feed removes at least a portion of the acid sites on the catalyst. The co-feed can be selected from the group of aniline, amines, cresol, anisol, and combinations thereof.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application claims priority to U.S. Provisional Patent No.61/488,782 filed on May 22, 2011.

FIELD

The present invention generally relates to catalysts, includingzeolites, for alkylation and other reactions. More specifically, thepresent invention relates to catalysts for the alkylation reactions oftoluene with methanol and/or formaldehyde.

BACKGROUND

A zeolite is a crystalline alumino-silicate that is well known for itsutility in several applications. Zeolites have been used indealkylation, transalkylation, isomerization, cracking,disproportionation, and dewaxing processes, among others. Itswell-ordered structure is composed of tetrahedral AlO₄ ⁻⁴ and SiO₄ ⁻⁴molecules bound by oxygen atoms that form a system of pores typically onthe order of 3 Å to 10 Å in diameter. These pores create a high internalsurface area and allow the zeolite to selectively adsorb certainmolecules while excluding others, based on the shape and size of themolecules. Thus, a zeolite can be categorized as a molecular sieve. Azeolite can also be termed a “shape selective catalyst.” The small poresof the zeolite can restrict reactions to certain transition states orcertain products, preventing shapes that do not fit the contours ordimensions of the pores.

The pores of a zeolite are generally occupied by water molecules andcations. Cations balance out the negative charge caused by trivalentaluminum cations which are coordinated tetrahedrally by oxygen anions. Azeolite can exchange its native cations for other cations; one exampleis the exchange of sodium ions for ammonium ions. In some ion-exchangedforms, such as the hydrogen form of a zeolite, the catalyst is stronglyacidic. These acidic active sites may be useful for alkylation as wellas many other reactions. For instance, zeolites can serve as a catalystfor Friedel-Crafts alkylations, replacing traditional aluminumtrichloride and other liquid acid catalysts that can be corrosive anddamaging to the reactor.

One alkylation reaction for which zeolite can be used as a catalyst isthe alkylation of toluene with methanol and/or formaldehyde to formstyrene. Styrene, also known as vinyl benzene, is an organic compoundhaving the chemical formula C₆H₅CHCH₂. The monomer styrene may bepolymerized to form the polymer polystyrene. Polystyrene is a plasticthat can form many useful products, including molded products and foamedproducts, all of which increase the need for production of styrene.

In the production of styrene, zeolite catalysts may be utilized. Thezeolite used in the production of styrene can be categorized as aheterogeneous acid catalyst. The zeolite is characterized asheterogeneous because it is in a different phase than the reactants. Thezeolite catalyst is solid and usually supported by an alumina or silicabinder to increase its mechanical stability inside the reactor bed.

Bulk zeolitic catalysts typically contain an abundance of acid sites. Inthe presence of alkylation reactions, however, these acid sites maycontribute to the production of unwanted by-products, such as xylenes.

Therefore, it would be desirable to reduce the amount of the acid siteson a zeolitic catalyst used in the production of styrene. It would alsobe desirable to use an alkylation catalyst capable of increasing theselectivity to styrene.

SUMMARY

The present invention in its many embodiments relates to a process ofmaking styrene. In an embodiment of the present invention, a process isprovided for making styrene including providing toluene, a co-feed, anda C₁ source to a reactor including a catalyst containing acid sites andreacting toluene with the C₁ source in the presence of the catalyst andthe co-feed to form a product stream including ethylbenzene and styrene.The co-feed is a base compound that reduces the number of active acidsites on the catalyst.

In an embodiment, either by itself or in combination with any otherembodiment, the C₁ source can be selected from the group of methanol,formaldehyde, formalin, trioxane, methylformcel, paraformaldehyde,methylal, dimethyl ether, and combinations thereof. The tolueneconversion can be at least 3 mol %. The selectivity to styrene can be atleast 10 mol % and the selectivity to ethylbenzene can be at least 10mol %.

In an embodiment, either by itself or in combination with any otherembodiment, catalyst comprises at least one promoter on a supportmaterial that can be selected from the group of Co, Mn, Ti, Zr, V, Nb,K, Cs, Ga, B, P, Rb, Ag, Na, Cu, Mg, Fe, Mo, Ce, and combinationsthereof.

In an embodiment, either by itself or in combination with any otherembodiment, the co-feed adds basic sites to the catalyst. Optionally,the co-feed removes at least a portion of the total number of activeacid sites on the catalyst by the molecules of the co-feed occupyingspatial volume near the acid sites of the catalyst. The co-feed can beadded to the catalyst prior to the toluene and the C1 source.Optionally, the co-feed can be simultaneously fed to the reactor withthe toluene and the C1 source. The co-feed can be selected from thegroup of aniline, amines, cresol, anisol, and combinations thereof. Theco-feed can be present in amounts of from 0.1 to 5.0 wt % based on thetotal weight of the feed. Optionally, the co-feed is present in amountsof from 0.5 to 1.0 wt % based on the total weight of the feed.

Another embodiment of the present invention includes a method ofpreparing a catalyst. The method includes providing a substrate and afirst solution including at least one promoter; contacting the substratewith the first solution; obtaining a catalyst including at least onepromoter and having an initial number of active acid sites; placing thecatalyst in an alkylation reactor; and contacting the catalyst in thealkylation reactor with a co-feed selected from the group of aniline,amines, cresol, anisol, and combinations thereof. The co-feed reducesthe number of active acid sites.

In an embodiment, either by itself or in combination with any otherembodiment, the substrate is a zeolite. The co-feed can be present inamounts of from 0.1 to 5.0 wt % based on the total weight of the feed.The co-feed can remove at least a portion of the acid sites on thecatalyst. The spatial volume near the acid sites of the catalyst can beoccupied by molecules of the co-feed. In yet another embodiment, aprocess is provided for producing styrene including providing toluene, aco-feed, and a C₁ source to a reactor including a catalyst containingacid sites and reacting toluene with the C₁ source in the presence ofthe catalyst and the co-feed to form a product stream includingethylbenzene and styrene. The C₁ source is selected from the group ofmethanol, formaldehyde, formalin, trioxane, methylformcel,paraformaldehyde, methylal, dimethyl ether, and combinations thereof,and the co-feed is selected from the group of aniline, amines, cresol,anisol, and combinations thereof. The co-feed can be present in amountsfrom 0.1 to 5.0 wt % based on the total weight of the feed and removesat least a portion of the acid sites on the catalyst. Molecules of theco-feed can occupy spatial volume near acid sites of the catalyst,thereby rendering such acid sites as inactive.

The various embodiments of the present invention can be joined incombination with other embodiments of the invention and the listedembodiments herein are not meant to limit the invention. Allcombinations of embodiments of the invention are enabled, even if notgiven in a particular example herein.

BRIEF DESCRIPTION OF DRAWINGS

FIG. 1 illustrates a flow chart for the production of styrene by thereaction of formaldehyde and toluene, wherein the formaldehyde is firstproduced in a separate reactor by either the dehydrogenation oroxidation of methanol and is then reacted with toluene to producestyrene.

FIG. 2 illustrates a flow chart for the production of styrene by thereaction of formaldehyde and toluene, wherein methanol and toluene arefed into a reactor, wherein the methanol is converted to formaldehydeand the formaldehyde is reacted with toluene to produce styrene.

DETAILED DESCRIPTION

The present invention relates to increasing the activity and/orselectivity in an alkylation process, specifically an alkylation oftoluene with methanol process. More specifically, the present inventionis related to the modification of a catalyst, such as a zeolitecatalyst, to reduce the number of acid sites on the catalyst. Also, thecatalyst is modified by the addition of a molecule having a more basiccharacter than that of toluene in a way that reduces the total number ofacid sites of the zeolite catalyst, such that by-product formation isinhibited and styrene selectivity is increased. Also, the presentinvention includes the addition of a molecule having a steric characterthat would allow the molecule to occupy spatial volume near the acidicsites of the zeolite which can render such acid sites as inactive.

In accordance with an embodiment of the current invention, toluene isreacted with a carbon source, which can be referred to as a C₁ source,capable of coupling with toluene to produce styrene and ethylbenzene. Inan embodiment, the C₁ source includes methanol or formaldehyde or amixture of the two. In an alternative embodiment, toluene is reactedwith one or more of the following: formalin (37-50% H₂CO in solution ofwater and MeOH), trioxane (1,3,5-trioxane), methylformcel (55% H₂CO inmethanol), paraformaldehyde, methylal (dimethoxymethane), and dimethylether. In a further embodiment, the C₁ source is selected from the groupof methanol, formaldehyde, formalin, trioxane, methylformcel,paraformaldehyde and methylal, dimethyl ether, and combinations thereof.

Formaldehyde can be produced either by the oxidation or dehydrogenationof methanol. In an embodiment, formaldehyde is produced by thedehydrogenation of methanol to produce formaldehyde and hydrogen gas.This reaction step produces a dry formaldehyde stream that may bepreferred, as it would not require the separation of the water prior tothe reaction of the formaldehyde with toluene. The dehydrogenationprocess is described in the equation below:

CH₃OH→CH₂O+H₂

Formaldehyde can also be produced by the oxidation of methanol toproduce formaldehyde and water. The oxidation of methanol is describedin the equation below:

2CH₃OH+O₂→2CH₂O+2H₂O

In the case of using a separate process to obtain formaldehyde, aseparation unit may then be used in order to separate the formaldehydefrom the hydrogen gas or water from the formaldehyde and unreactedmethanol prior to reacting the formaldehyde with toluene for theproduction of styrene. This separation would inhibit the hydrogenationof the formaldehyde back to methanol. Purified formaldehyde could thenbe sent to a styrene reactor and the unreacted methanol could berecycled.

Although the reaction has a 1:1 molar ratio of toluene and the C₁source, the ratio of the C1 source and toluene feedstreams is notlimited within the present invention and can vary depending on operatingconditions and the efficiency of the reaction system. If excess tolueneor C₁ source is fed to the reaction zone, the unreacted portion can besubsequently separated and recycled back into the process. In oneembodiment the ratio of toluene:C₁ source can range from between 100:1to 1:100. In alternate embodiments the ratio of toluene:C₁ source canrange from 50:1 to 1:50; from 20:1 to 1:20; from 10:1 to 1:10; from 5:1to 1:5; from 2:1 to 1:2. In a specific embodiment, the ratio oftoluene:C_(i) source can range from 2:1 to 5:1.

The acidity of zeolitic materials may present problems in catalyticperformance, specifically in the alkylation of toluene with methanoland/or formaldehyde. The acidity, as well as the basicity, of thezeolitic material is dependent upon the amount of acid sites on thezeolitic material. The addition of a basic compound on or within orattached to the catalyst can increase the basic nature of the catalystand reduce the effective acidity of the catalyst.

In an embodiment, the reactants, toluene and the C1 source, are combinedwith a co-feed having a basic property. In an embodiment, the co-feed isselected from basic compounds. In an embodiment, the co-feed is selectedfrom the group of aniline, amines, cresol, anisol, and combinationsthereof. The co-feed may be combined with the reactants in any desiredamounts. In an embodiment, the co-feed is added in amounts ranging from0.1 to 5.0 wt % based on the total weight of the feed. In anotherembodiment, the co-feed is added in amounts ranging from 0.25 to 2.5 wt% based on the total weight of the feed, optionally from 0.5 to 1.0 wt %based on the total weight of the feed.

Upon contact with the co-feed, at least a portion of the total number ofacid sites on the zeolite may be selectively poisoned or masked by theco-feed. In an embodiment, the co-feed may have a more basic characterthan that of toluene. In an embodiment, the co-feed may have a stericcharacter that may allow at least a portion of the co-feed to occupyspatial volume near the acid sites of the zeolite. In a furtherembodiment, the addition of the co-feed may alter the structuraldimensions of the catalyst, resulting in the catalyst having an alteredshape selectivity.

An improvement in side chain alkylation selectivity may be achieved bytreating a molecular sieve zeolite catalyst with chemical compounds toinhibit the external acidic sites and to minimize aromatic alkylation onthe ring positions. Another means of improvement of side chainalkylation selectivity can be to impose restrictions on the catalyststructure to facilitate side chain alkylation. In one embodiment thecatalyst used in an embodiment of the present invention is a basic orneutral catalyst.

For the present invention, the catalyst can be a zeolite, but can alsobe a non-zeolite. A zeolite is generally a porous, crystallinealumino-silicate, and it can be formed either naturally orsynthetically. One method of forming a synthetic zeolite is thehydrothermal digestion of silica, alumina, sodium or other alkyl metaloxide, and an organic templating agent. The amounts of each reactant andthe inclusion of various metal oxides can lead to several differentsynthetic zeolite compositions. Furthermore, a zeolite is commonlyaltered through a variety of methods to adjust characteristics such aspore size, structure, activity, acidity, and silica/alumina molar ratio.Thus, a number of different forms of zeolite are available.

Zeolite materials suitable for this invention may include silicate-basedzeolites and amorphous compounds such as faujasites, mordenites, etc.Silicate-based zeolites are made of alternating SiO₄ ⁻⁴ and MO_(x)tetrahedra, where M is an element selected from the Groups 1 through 16of the Periodic Table (new IUPAC). These types of zeolites have 4, 6, 8,10, or 12-membered oxygen ring channels. An example of the zeolites ofthe present invention can include faujasites, such as an X-type orY-type zeolite and zeolite beta. Zeolite-like materials can also be aneffective substrate. Alternate molecular sieves also contemplated arezeolite-like materials such as the crystalline silicoaluminophosphates(SAPO) and the aluminophosphates (ALPO) and the like.

Another method of altering a zeolite is by ion-exchange. For example,the hydrogen form of a zeolite can be produced by ion-exchanging betazeolite with ammonium ions. Ion exchange may be performed byconventional ion exchange methods in which sodium, hydrogen, or otherinorganic cations that may be typically present in a substrate are atleast partially replaced via a fluid solution. In an embodiment, thefluid solution can include any medium that will solubilize the cationwithout adversely affecting the substrate. Increasing the amount ofsilica relative to alumina can have the effect of increasing thecatalyst hydrophobicity.

In an embodiment, the ion exchange is performed by heating a solutioncontaining any promoter selected from the group of Co, Mn, Ti, Zr, V,Nb, K, Cs, Ga, B, P, Rb, Ag, Na, Cu, Mg, Fe, Mo, Ce, and anycombinations thereof in which the promoter(s) is(are) solubilized in thesolution, which may be heated, and contacting the solution with thesubstrate. In another embodiment, the ion exchange includes heating asolution containing any one selected from the group of Ce, Cu, P, Cs, B,Co, Ga, and any combinations thereof. In an embodiment, the solution isheated to temperatures ranging from 50 to 120° C. In another embodiment,the solution is heated to temperatures ranging from 80 to 100° C.

A variety of zeolites and non-zeolites are available for use in thepresent invention. The various catalysts listed in this disclosure arenot meant to be an exhaustive list, but is meant to indicate the type ofcatalysts for which may be useful in the present invention.

The catalytic reaction systems suitable for this invention can includeone or more of the zeolite or amorphous materials modified for sidechain alkylation selectivity. A non-limiting example can be a zeolitepromoted with one or more metal ion of the following: Co, Mn, Ti, Zr, V,Nb, K, Cs, Ga, B, P, Rb, Ag, Na, Cu, Mg, Fe, Mo, Ce, and anycombinations thereof. In general the promoter exchanges with Na withinthe zeolite or amorphous material. The promoter can also be attached tothe zeolite or amorphous material in an occluded manner. In anembodiment the amount of promoter is determined by the amount needed toyield less than 0.5 mol % of ring alkylated products such as xylenesfrom a coupling reaction of toluene and a C1 source.

In an embodiment, the catalyst contains greater than 0.1 wt % of atleast one promoter based on the total weight of the catalyst. In anotherembodiment, the catalyst contains up to 5 wt % of at least one promoter.In a further embodiment, the catalyst contains from 1 to 3 wt % of atleast one promoter.

As used herein, the term “metal ion” is meant to include all activemetal ions and similar species, such as metal oxides, nanoparticles, andmixed metal oxide phases, capable of being added to a catalyst, or to abinder and enabling the binder to reduce the acidity, or increase thebasicity or basic strength, of the supported catalyst without adverselyaffecting the catalyst that it supports or causing significantby-product formation at reaction conditions.

The metal ion can be added to the zeolite, or non-zeolite, in the amountof 0.1% to 50%, optionally 0.1% to 20%, optionally 0.1% to 5%, by weightof the zeolite, or non-zeolite. The metal ion can be added to thezeolite, or non-zeolite, by any means known in the art. Generally, themethod used is incipient wetness impregnation, wherein the metal ionprecursor is added to an aqueous solution, which solution is poured overa zeolite. After sitting for a specified period, the zeolite is driedand calcined, such that the water is removed with the metal iondeposited on the surface of the zeolite. The ion-modified zeolite canthen be mixed with a binder, or another catalyst, by any means known inthe art. The mixture is shaped via extrusion or some other method into aform such as a pellet, tablet, cylinder, cloverleaf, dumbbell,symmetrical and asymmetrical polylobates, sphere, or any other shapesuitable for the reaction bed. The shaped form is then usually dried andcalcined. Drying can take place at a temperature of from 100° C. to 200°C. Calcining can take place at a temperature of from 400° C. to 900° C.in a substantially dry environment.

The powder form of a zeolite and other catalysts may be unsuitable foruse in a reactor, due to a lack of mechanical stability, makingalkylation and other desired reactions difficult. To render a catalystsuitable for the reactor, it can be combined with a binder to form anaggregate, such as a zeolite aggregate. The binder-modified zeolite,such as a zeolite aggregate, will have enhanced mechanical stability andstrength over a zeolite that is not combined with a binder, or otherwisein powder form. The aggregate can then be shaped or extruded into a formsuitable for the reaction bed. The binder can desirably withstandtemperature and mechanical stress and ideally does not interfere withthe reactants adsorbing to the catalyst. In fact, it is possible for thebinder to form macropores, much greater in size than the pores of thecatalyst, which provide improved diffusional access of the reactants tothe catalyst.

Binder materials that are suitable for the present invention include,but are not limited to, silica, alumina, titania, zirconia, zinc oxide,magnesia, boria, silica-alumina, silica-magnesia, chromia-alumina,alumina-boria, silica-zirconia, silica gel, clays, kaolin,montmorillonite, modified clays, similar species, and any combinationsthereof. The most frequently used binders are amorphous silica andalumina, including gamma-, eta-, and theta-alumina. It should be notedthat a binder can be used with many different catalysts, includingvarious forms of zeolite and non-zeolite catalysts that requiremechanical support.

The reactants can enter the reactor via a single inlet or separateinlets. The reactants can be delivered to the reaction bed in thegaseous phase, the liquid phase, a combination of liquid and gaseousphase, the supercritical phase, or a combination of liquid andsupercritical phases. The reaction conditions, including reactor type,pressure, temperature, liquid hourly space velocity (LHSV), and benzeneto ethylene ratio depend in part on the phase in which the alkylation isto occur.

The operating conditions of the reactors and separators will be systemspecific and can vary depending on the feedstream composition and thecomposition of the product streams. The reactor for the reactions ofmethanol to formaldehyde and toluene with formaldehyde will operate atelevated temperatures and may contain a basic or neutral catalystsystem. The temperature can range in a non-limiting example from 250° C.to 750° C., optionally from 300° C. to 500° C., optionally from 375° C.to 450° C. The pressure can range in a non-limiting example from 0.1 atmto 70 atm, optionally from 0.1 atm to 35 atm, optionally from 0.1 atm to10 atm, optionally from 0.1 atm to 5 atm.

Inert diluents such as helium and nitrogen may be included in the feedto adjust the gas partial pressures. The reaction pressure is not alimiting factor regarding the present invention and any suitablecondition is considered to be within the scope of the invention.

Any suitable space velocity, within the short reaction time parametersof the present invention, can be considered to be within the scope ofthe invention.

In FIG. 1 there is a simplified flow chart of one embodiment of thestyrene production process described above. In this embodiment, a firstreactor (2) is either a dehydrogenation reactor or an oxidation reactor.This reactor is designed to convert the first methanol feed (1) intoformaldehyde. The gas product (3) of the reactor is then sent to a gasseparation unit (4) where the formaldehyde is separated from anyunreacted methanol and unwanted byproducts. Any unreacted methanol (6)can then be recycled back into the first reactor (2). The byproducts (5)are separated from the clean formaldehyde (7).

In one embodiment the first reactor (2) is a dehydrogenation reactorthat produces formaldehyde and hydrogen and the separation unit (4) is amembrane capable of removing hydrogen from the product stream (3).

In an alternate embodiment the first reactor (2) is an oxidative reactorthat produces product stream (3) comprising formaldehyde and water. Theproduct stream (3) comprising formaldehyde and water can then be sent tothe second reactor (9) without a separation unit (4).

The formaldehyde feed stream (7) is then reacted with a feed stream oftoluene (8) and a co-feed stream (16) in a second reactor (9). Thetoluene and formaldehyde react to produce styrene. The product (10) ofthe second reactor (9) may then be sent to an optional separation unit(11) where any unwanted byproducts (15) such as water can separated fromthe styrene, unreacted formaldehyde and unreacted toluene. Any unreactedformaldehyde (12) and the unreacted toluene (13) can be recycled backinto the reactor (9). A styrene product stream (14) can be removed fromthe separation unit (11) and subjected to further treatment orprocessing if desired.

The operating conditions of the reactors and separators will be systemspecific and can vary depending on the feedstream composition and thecomposition of the product streams. The reactor (9) for the reaction oftoluene and formaldehyde will operate at elevated temperatures. Thetemperature can range in a non-limiting example from 250° C. to 750° C.,optionally from 300° C. to 500° C., optionally from 375° C. to 450° C.The pressure can range in a non-limiting example from 0.1 atm to 70 atm,optionally from 0.1 atm to 35 atm, optionally from 0.1 atm to 10 atm,optionally from 0.1 atm to 5 atm.

FIG. 2 is a simplified flow chart of another embodiment of the styreneprocess discussed above. A C₁ source containing feed stream (21) is fedalong with a feed stream of toluene (22) and a co-feed stream (31) in areactor (23). Toluene and the C₁ source then react to produce styrene.The product (24) of the reactor (23) may then be sent to an optionalseparation unit (25) where any unwanted byproducts (26) can be separatedfrom the styrene, and any unreacted C1 source, unreacted methanol,unreacted formaldehyde and unreacted toluene. Any unreacted methanol(27), unreacted formaldehyde (28) and the unreacted toluene (29) can berecycled back into the reactor (23). A styrene product stream (30) canbe removed from the separation unit (25) and subjected to furthertreatment or processing if desired.

The operating conditions of the reactors and separators will be systemspecific and can vary depending on the feedstream composition and thecomposition of the product streams. The reactor (23) for the reactionsof methanol to formaldehyde and toluene with formaldehyde will operateat elevated temperatures. The temperature can range in a non-limitingexample from 250° C. to 750° C., optionally from 300° C. to 500° C.,optionally from 375° C. to 450° C. The pressure can range in anon-limiting example from 0.1 atm to 70 atm, optionally from 0.1 atm to35 atm, optionally from 0.1 atm to 10 atm, optionally from 0.1 atm to 5atm.

Upon deactivation, the zeolite may require a regeneration procedure tobe performed. Some methods of regenerating a zeolite include heating toremove adsorbed materials, ion exchanging with sodium to remove unwantedcations, or a pressure swing to remove adsorbed gases. One solutioninvolves flushing the catalyst with benzene. Other solutions generallyinvolve processing the catalyst at high temperatures using regenerationgas and oxygen. According to one procedure, a zeolite beta can beregenerated by heating the catalyst first to a temperature in excess of300° C. in an oxygen-free environment. Then an oxidative regenerationgas can be supplied to the catalyst bed with oxidation of a portion of arelatively porous coke component to produce an exotherm moving throughthe catalyst bed. Either the temperature or the oxygen content of thegas can be progressively increased to oxidize a porous component of thecoke. Again, regeneration gas can be supplied, wherein the gas haseither increased oxygen content or increased temperature to oxidize aless porous refractory component of the coke. The regeneration processcan be completed by passing an inert gas through the catalyst bed at areduced temperature.

In one embodiment, the present invention is for an alkylation processcontaining a catalyst, wherein toluene, a C1 source, and a co-feed arefed to a reactor containing the catalyst wherein the co-feed removes atleast a portion of the total number of acid sites on the catalyst. Inanother embodiment, the present invention is for an alkylation processcontaining a catalyst, wherein toluene, a C1 source, and a co-feed arefed to a reactor containing the catalyst wherein the co-feed adds basicsites to the catalyst. In yet another embodiment, the present inventionis for an alkylation process containing a catalyst, wherein toluene, aC1 source, and a co-feed are fed to a reactor containing the catalystwherein the molecules of the co-feed can occupy spatial volume near theacidic sites of the zeolite.

EXAMPLES

A catalyst promoted with both Cs and B was used in an ATM reaction withthe addition of triethylamine in amounts of 0 ppm, 500 ppm, and 1000ppm. The reactions each had a Tolene:MeOH ratio of 1.0, a LHSV of 1.5hr⁻¹, and temperature of 420° C., pressure of 1.3 psig and a 2.5 secondcontact time. The results are shown in Table 1.

The addition of triethylamine increased the toluene conversion and didnot decrease styrene selectivity. The addition of 500 ppm triethylamineincreased toluene conversion by about 15% without an increase inmethanol conversion. With 1000 ppm triethylamine the toluene conversionincreased by about 20% and did not indicate a reduction in tolueneconversion throughout the run thereby giving a reduced deactivationrate. The methanol conversion increased at the 1000 ppm triethylamine.The cumene and alpha methyl styrene remained low and within acceptableranges.

TABLE 1 Triethyl- Time On amine Stream (ppm) (hh:mm) X_(Tol) S_(Bz)S_(Xyl) S_(EB) S_(Sty) S_(Cumene) S_(ams) X_(MeOH) None 1:44 9.7 0.70.140 76.5 20.4 1.80 0.4 48.9 2:10 9.6 0.7 0.144 75.3 21.7 1.76 0.4 45.32:46 9.5 0.7 0.151 75.0 22.0 1.73 0.4 48.0 4:09 10.0 0.5 0.158 73.9 22.12.49 0.6 46.0 5:13 8.3 0.5 0.214 74.8 21.1 2.52 0.5 48.6  500 1:11 11.80.9 0.928 73.8 20.7 2.42 0.6 50.2 1:44 12.2 0.6 0.667 74.2 21.0 2.41 0.648.3 2:14 12.3 0.7 0.535 74.3 21.0 2.35 0.6 61.7 2:49 12.2 0.9 0.47573.4 21.5 2.47 0.7 30.4 4:21 7.0 0.7 0.220 77.7 19.9 1.19 0.2 43.3 5:216.4 0.7 0.238 78.2 19.4 1.20 0.2 41.2 1000 1:05 12.0 0.8 0.142 77.3 19.51.99 0.3 70.2 1:44 12.3 0.6 0.147 75.6 20.8 2.17 0.4 74.5 2:17 12.5 0.60.148 75.6 20.9 2.14 0.4 63.5 2:56 11.6 0.6 0.162 74.1 22.2 2.21 0.469.6 4:01 12.1 0.5 0.183 73.6 22.5 2.33 0.5 59.6 5:03 12.2 0.4 0.20172.8 23.1 2.37 0.6 58.4

Procedure used to produce the cesium ion-exchanged zeolite material: Aglass cylinder (2″ inside diameter), fitted with a sintered glass diskand stopcock at the lower end, was charged with 544-HP zeolite (100 g,W.R. Grace) and CsOH (400 mL, 1.0 M in water). The mixture was thenbrought to 90° C. and allowed to stand for 4 h. The liquid was drainedfrom the zeolite material and another aliquot of CsOH (400 mL of 1.0 Msolution in water) was added and allowed to stand for 3 hours at 90° C.The liquid was drained from the zeolite material and another aliquot ofCsOH (400 mL of 1.0 M solution in water) was added and allowed to standfor 15 hours at 90° C. The liquid was drained from the zeolite materialand dried at 150° C. for 1.5 hours.

Deposition of 1.4 wt % boron onto cesium ion-exchanged zeolite material:The cesium ion-exchanged zeolite material (35 g) was treated with asolution of boric acid (2.8 g) dissolved in acetone (500 mL) at roomtemperature for 2 hours. The (Cs, B)/X material was then dried at 110°C. for 20 hours.

The term “conversion” refers to the percentage of reactant (e.g.toluene) that undergoes a chemical reaction.

X _(Tol)=conversion of toluene (mol %)=(Tol_(in)−Tol_(out))/Tol_(in)

X _(MeOH)=conversion of methanol to styrene+ethylbenzene (mol %)

The term “molecular sieve” refers to a material having a fixed,open-network structure, usually crystalline, which may be used toseparate hydrocarbons or other mixtures by selective occlusion of one ormore of the constituents, or may be used as a catalyst in a catalyticconversion process.

Use of the term “optionally” with respect to any element of a claim isintended to mean that the subject element is required, or alternatively,is not required. Both alternatives are intended to be within the scopeof the claim. Use of broader terms such as comprises, includes, having,etc. should be understood to provide support for narrower terms such asconsisting of, consisting essentially of, comprised substantially of,etc.

The term “regenerated catalyst” refers to a catalyst that has regainedenough activity to be efficient in a specified process. Such efficiencyis determined by individual process parameters.

The term “regeneration” refers to a process for renewing catalystactivity and/or making a catalyst reusable after its activity hasreached an unacceptable/inefficient level. Examples of such regenerationmay include passing steam over a catalyst bed or burning off carbonresidue, for example.

The term “selectivity” refers to the relative activity of a catalyst inreference to a particular compound in a mixture. Selectivity isquantified as the proportion of a particular product relative to allother products.

S _(Sty)=selectivity of toluene to styrene (mol%)=Sty_(out)/Tol_(converted)

S _(Bz)=selectivity of toluene to benzene (mol%)=Benzene_(out)/Tol_(converted)

S _(EB)=selectivity of toluene to ethylbenzene (mol%)=EB_(out)/Tol_(converted)

S _(Xyl)=selectivity of toluene to xylenes (mol%)=Xylenes_(out)/Tol_(converted)

S _(Sty+EB)(MEOH)=selectivity of methanol to styrene+ethylbenzene (mol%)=(Sty_(out)+EB_(out))/MeOH_(converted)

The term “zeolite” refers to a molecular sieve containing a silicatelattice, usually in association with some aluminum, boron, gallium,iron, and/or titanium, for example. In the following discussion andthroughout this disclosure, the terms molecular sieve and zeolite willbe used more or less interchangeably. One skilled in the art willrecognize that the teachings relating to zeolites are also applicable tothe more general class of materials called molecular sieves.

The various embodiments of the present invention can be joined incombination with other embodiments of the invention and the listedembodiments herein are not meant to limit the invention. Allcombinations of various embodiments of the invention are enabled, evenif not given in a particular example herein.

While illustrative embodiments have been depicted and described,modifications thereof can be made by one skilled in the art withoutdeparting from the spirit and scope of the disclosure. Where numericalranges or limitations are expressly stated, such express ranges orlimitations should be understood to include iterative ranges orlimitations of like magnitude falling within the expressly stated rangesor limitations (e.g., from about 1 to about 10 includes, 2, 3, 4, etc.;greater than 0.10 includes 0.11, 0.12, 0.13, etc.).

Depending on the context, all references herein to the “invention” mayin some cases refer to certain specific embodiments only. In other casesit may refer to subject matter recited in one or more, but notnecessarily all, of the claims. While the foregoing is directed toembodiments, versions and examples of the present invention, which areincluded to enable a person of ordinary skill in the art to make and usethe inventions when the information in this patent is combined withavailable information and technology, the inventions are not limited toonly these particular embodiments, versions and examples. Also, it iswithin the scope of this disclosure that the embodiments disclosedherein are usable and combinable with every other embodiment disclosedherein, and consequently, this disclosure is enabling for any and allcombinations of the embodiments disclosed herein. Other and furtherembodiments, versions and examples of the invention may be devisedwithout departing from the basic scope thereof and the scope thereof isdetermined by the claims that follow.

1-14. (canceled)
 15. A method of preparing a catalyst, comprising:providing a substrate; providing a first solution comprising at leastone promoter; contacting the substrate with the first solution;obtaining a catalyst comprising at least one promoter and having a firstnumber of active acid sites; placing the catalyst in an alkylationreactor; and contacting the catalyst in the alkylation reactor with aco-feed selected from the group consisting of aniline, amine, cresol,and anisol, and combinations thereof; wherein the contacting of thesubstrate with the solution subjects the substrate to the addition of atleast one promoter; wherein the contacting the catalyst with the co-feedreduces the number of active acid sites of the catalyst.
 16. The methodof claim 15, wherein the substrate is a zeolite.
 17. The method of claim15, wherein the co-feed is present in amounts of from 0.1 to 5.0 wt %based on the total weight of he feed to the alkylation reactor.
 18. Themethod of claim 15, wherein the co-feed reduces the acidity of thecatalyst.
 19. The method of claim 15, wherein, after contacting thecatalyst with the co-feed, spatial volume near the acid sites of thecatalyst are occupied by molecules of the co-feed.
 20. The method ofclaim 15, wherein the co-feed is a base compound selected from the groupconsisting of aniline, cresol, anisol, and combinations thereof.
 21. Themethod of claim 20, wherein the catalyst is an X-zeolite and the atleast one promoter includes Cs.
 22. The method of claim 15, wherein thecatalyst is an X-zeolite and the at least one promoter includes Cs. 23.The method of claim 15, wherein the at least one promoter is selectedfrom the group consisting of Co, Mn, Ti, Zr, V, Nb, K, Cs, Ga, B, P, Rb,Ag, Na, Cu, Mg, Fe, Mo, Ce, and combinations thereof.
 24. The method ofclaim 15, wherein the catalyst includes greater than 0.1 weight percentof the at least one promoter.
 25. The method of claim 15, wherein theco-feed adds basic sites to the catalyst.
 26. The method of claim 15,wherein the co-feed is more basic than toluene.
 27. The method of claim15, wherein the substrate is a mordenite or faujasite.
 28. The method ofclaim 15, wherein the substrate is an X-type zeolite, a Y-type zeolite,or a zeolite beta.
 29. The method of claim 15, wherein the substrate isa crystalline silicoaluminophosphates (SAPO) or an aluminophosphates(ALPO).